EP1492728B1 - Procede de production d'une saumure d'halogenure - Google Patents

Procede de production d'une saumure d'halogenure Download PDF

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Publication number
EP1492728B1
EP1492728B1 EP03716990A EP03716990A EP1492728B1 EP 1492728 B1 EP1492728 B1 EP 1492728B1 EP 03716990 A EP03716990 A EP 03716990A EP 03716990 A EP03716990 A EP 03716990A EP 1492728 B1 EP1492728 B1 EP 1492728B1
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Prior art keywords
fluid
water
alkali
gal
suspended solids
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German (de)
English (en)
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EP1492728A1 (fr
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Raymond D. Symens
Lyle H. Howard
Surendra Mishra
Thomas William Polkinghorn
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Tetra Technologies Inc
Tetra Tech Inc
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Tetra Technologies Inc
Tetra Tech Inc
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    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
    • C01D3/00—Halides of sodium, potassium or alkali metals in general
    • C01D3/04—Chlorides
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
    • C01D3/00—Halides of sodium, potassium or alkali metals in general
    • C01D3/10—Bromides
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
    • C01D3/00—Halides of sodium, potassium or alkali metals in general
    • C01D3/12—Iodides
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
    • C01F11/00—Compounds of calcium, strontium, or barium
    • C01F11/20—Halides
    • C01F11/34—Bromides

Definitions

  • the present invention relates to a method for producing a halide brine. More specifically the invention relates to a method for producing a halide brine in a conventional reactor.
  • Halide brines are commonly used in industry for various applications, drilling fluids, textile treatment, photographic emulsion, cooling systems, deicing, and dust control, for example.
  • the production of halide brines typically required production of intermediate halide acids.
  • the production of halide acid from halogen and hydrogen requires expensive equipment.
  • intermediate halide acids are formed. These intermediate acids can be corrosive and possibly produce volatile gases thereby requiring expensive equipment for handling and maintenance. Thus the formation of intermediate halide acids during the production of metal halide brines requires expensive capital equipment.
  • the present invention relates to an inexpensive and simple method for rapidly manufacturing halide brines in large commercial quantities using conventional equipment.
  • an alkali and a reducing agent are added to an aqueous fluid having a density greater than 8.30 lb/gal. (0.994 kg/L), water, sea water or waste water for example.
  • a reducing agent can be in liquid form or in gaseous state that goes into solution when added to the aqueous fluid.
  • the resulting liquid is contacted with a halogen to form a halide brine.
  • Typical halogens used in the process of making the more useful brines are chlorine and bromine to produce the commonly used chloride and bromide brines. This invention eliminates the additional costs that are associated with the production of intermediate halide acids.
  • the aqueous fluid comprises water from various sources, essentially pure water, tap water, sea water, river water, pond water, standing water, waste water, brackish water, or combinations thereof.
  • the water is a clear water.
  • the alkali can be selected from alkali metal hydroxides, alkali earth metal oxides, alkali earth metal hydroxides, base metal oxides, base metal hydroxides, and a combination thereof.
  • the metal source of the base metal oxides and base metal hydroxides is selected from iron, zinc, copper, nickel, cadmium, cobalt, aluminum, manganese, chromium, and combinations thereof.
  • the earth metal source of the alkali earth metal oxides and alkali earth metal hydroxides can be selected from calcium, magnesium, strontium and combinations thereof.
  • the reducing agent can be ammonia.
  • the reducing agent can be acetaldehyde.
  • An alternative reducing agent can be acetic acid.
  • the method of this invention takes place in a conventional reactor, wherein a halogen is converted directly to a halide brine eliminating the need for producing an intermediate halide acid.
  • solids are present in the initial aqueous fluid stream such as waste waters.
  • the preferred method comprises a further step of separating suspended solids from the beginning fluid prior to entering the reactor.
  • the step of separating suspended solids from the final fluid can occur at the end of the reaction process.
  • separation of suspended solids occurs both prior to the aqueous fluid entering the reactor as well as after the reacted fluid leaves the reactor.
  • the separation of suspended solids from the fluid can be performed in a variety of separators including a gravity filter, a clarifier, a centrifuge, a vacuum filter or a pressure filter. Any suspended solids within the final halide brine fluid can be separated from the fluid after the halogen has reacted with the reaction fluids by know separation techniques.
  • An alternative method for producing halide brine comprises adding an alkali to an aqueous fluid having a density greater than 8.30 lb/gal. (0.994 kg/L.) A reducing agent is then added to the resulting fluid and the combined mixture of alkali, reducing agent and aqueous fluid is contacted with a halogen to form a halide brine.
  • the reducing agent is added first to the aqueous fluid and then the alkali is charged into the reactor.
  • the resulting fluid is contacted with halogen to form a halide brine.
  • these steps are performed in a conventional reactor.
  • the Figure illustrates a schematic of a halogen brine reactor system.
  • the present invention relates to an innovative method for the direct conversion of a halogen to a halide brine in a conventional reactor such as a simple mixing tank.
  • a conventional reactor such as a simple mixing tank.
  • the stage of producing intermediate halide acids is eliminated thereby eliminating the necessity of expensive equipment.
  • the method of this invention can be used to produce a variety of halide brines, calcium chloride or calcium bromide for example, using a conventional reactor, from various halogens including but not limited to bromine, chlorine and iodine.
  • the description of the schematic refers to the production of calcium bromide.
  • aqueous fluid 22 having a density greater than 8.30 lb/gal. (0.994 kg/L), water for example, is charged into a conventional reactor 20.
  • the aqueous fluid can comprise water from various sources, essentially pure water, tap water, sea water, river water, pond water, standing water, waste water from process plants, brackish water, or combinations thereof.
  • Sea water is one preferred aqueous fluid, particularly in the formation of high density brines used for drilling fluids.
  • the aqueous fluid is a clear water. If the water is not clear, a separator can be used to separate suspended solids from the beginning fluid prior to entering the reactor 20. Alternatively, separating suspended solids from the final fluid can occur at the end of the reaction process or, if necessary because of "dirty" water, both prior to the reaction and after the halogen brine is produced.
  • an alkali 24 (lime is used in the example depicted in the schematic) is added to the aqueous fluid 22 in a conventional reactor.
  • the alkali 24 can be selected from alkali metal hydroxides, alkali earth metal oxides, alkali earth metal hydroxides, base metal oxides, base metal hydroxides, and combinations thereof.
  • the alkali metal hydroxides can be selected from sodium hydroxide and potassium hydroxide.
  • the metal source of the base metal oxides and base metal hydroxides is selected from iron, zinc, copper, nickel, cadmium, cobalt, aluminum, manganese, chromium, and combinations thereof.
  • the metal source of the alkali earth metal oxides and alkali earth metal hydroxides can be selected from calcium, magnesium, strontium, and combinations thereof.
  • the alkali is in an aqueous fluid form, a lime slurry for example, as shown in the schematic.
  • a reducing agent 42 ammonia for example, is added to the aqueous fluid 22 in the reactor 20, either after the addition of the alkali or simultaneously along with the alkali 24.
  • the reducing agent 42 can be acetaldehyde.
  • Another alternative reducing agent is acetic acid.
  • the reducing agent can be in liquid form or a gaseous form that enters into solution upon being charged to the conventional reactor.
  • the reducing agent is in a liquid form, such as aqueous ammonia.
  • halogen 32 is charged from a storage tank 30 to the conventional reactor 20 to combine with the alkali 24 and reducing agent 42 to form a halide brine 65, calcium bromide for example.
  • Typical halogens used in the process of making the more useful brines are chlorine and bromine to produce the commonly used chloride and bromide brines.
  • the halogen is added until the resulting fluid has a density of at least 8.5 lb/gal (1.02 kg/L)
  • the selection of the specific alkali, reducing agent and halogen depends on the final required density of the halide brine.
  • the choice of aqueous fluid, alkali, reducing agent, and halogen, as well as, the concentrations of each of these chemicals in the starting solutions is determined by the required density of the final product.
  • seawater readily available in offshore operations, comprises a density greater than tap water, it is a good aqueous fluid source to produce brine of final density greater than 9.0 lb/gal. (1.08 kg/L.)
  • the reactor used in this method is a conventional reactor.
  • the halogen used is chlorine.
  • the mixture of aqueous fluid, alkali, and reducing agent in the conventional reactor is contacted with chlorine to increase the density to at least 8.5 lb/gal. (1.02 kg/L).
  • the fluid is contacted with bromine to increase the density to at least 10.0 lb/gal. (1.20 kg/L).
  • any suspended solids can be separated from the resulting fluid by conventional means.
  • the halogen used is bromine.
  • the alkali can be lime added to a water having a density greater than 8.30 lb/gal. (0.994 kg/L.)
  • the reducing agent selected for this process is ammonia.
  • the mixture of water lime and ammonia in the conventional reactor is contacted with bromine to increase the density to at least 10.0 lb/gal. (1.20 kg/L).
  • the fluid is contacted with bromine to increase the density to at least 10.0 lb/gal. (1.20 kg/L). Again, any suspended solids can be separated from the resulting fluid by conventional means.
  • both the bromine storage tank 30 and the reactor 20 vent to one or more scrubbers 50, 55 to scrub or remove any small amounts of free gases that may occur, bromine or ammonia, for example.
  • a heat exchanger 80 is used to cool the reaction fluids so that optimum temperatures are maintained to produce the desired halide brine and minimize evaporation of bromine or chlorine.
  • the temperature can easily increase to higher than 150°F (65.6°C) instantaneously.
  • the method of producing a halide brine comprises adding an alkali to an aqueous fluid having a density greater than 8.30 lb/gal. (0.994 kg/L).
  • the alkali is selected from alkali metal hydroxides, alkali earth metal oxides, alkali earth metal hydroxides, base metal oxides, base metal hydroxides, and a combination thereof.
  • a reducing agent is then added while maintaining the temperature at 68°F (20°C) or above; the reducing agent is selected from a group consisting of ammonia, acetaldehyde, acetic acid, and combinations thereof.
  • the fluid resulting from mixture of alkali, aqueous fluid having a density greater than 8.30 lb/gal., and reducing agent is contacted with a halogen to increase the density to at least 8.5 Ib/gal. (1.02 kg/L). As in the previously described embodiments, this reaction is performed in a conventional reactor.
  • the method of producing halide brines according to this invention can be a batch process or a continuous process.
  • halide brine production is a batch process
  • predetermined amounts of raw materials are added into the reactor to produce a fixed amount of the halide brine, calcium bromide for example.
  • the product is removed from the reactor before adding the raw materials for the next batch.
  • additional lime 24 may be added as bromine or other halogen is charged.
  • the additional alkali 24 is carefully added to control the reaction so that substantially all the halogen is consumed within the reactor.
  • the charge of alkali, reducing agent, halogen and additional alkali 24 is carefully monitored and controlled throughout the process for the same reason.
  • both the pH and the oxidation-reduction potential (ORP) are also monitored so that the end product is within the target pH and ORP for the halide brine being produced.
  • suspended solids are present in both the initial aqueous fluid stream such as dirt, in waste waters, as well as, the end product which may also have unconsumed alkali or un-reacted materials.
  • One preferred method comprises the separation of suspended solids both prior to the aqueous fluid entering the reactor, as well as, after the reacted fluid leaves the reactor.
  • the separation of suspended solids from the fluid can be performed in various separators 70 including a gravity filter, a clarifier, a centrifuge, a vacuum filter or a pressure filter.
  • the resulting halide brine 65 is cooled down in the heat exchanger 80 and then residual solids are removed using a separator or filter 70 prior to being sent to a stripper 60 to remove any residual ammonia.
  • calcium bromide is produced by combining hydrated lime and ammonia in an aqueous fluid and then reacting elemental bromine with the resulting mixture.
  • the reactions that take place are exothermic reactions generating large amounts of heat. This excess heat can be removed by a heat exchanger system.
  • lime and ammonia are added to an aqueous fluid having a density greater than 8.30 lb/gal. (0.994 kg/L).
  • bromine is charged into the reactor 20 to increase the density to at least 9.0 lb/gal. (1.08 kg/L).
  • Additional lime may be added to consume excess bromine and the reaction fluids may be cooled down by recycling them through a heat exchanger.
  • any suspended solids are separated from the desired end product, calcium bromide, by a filter and stripped of any excess ammonia in a stripper.
  • an alkali is charged to sea water in a conventional reactor such as a mixing tank.
  • a reducing agent can be charged to the reactor and the resulting mixture of alkali, reducing agent and sea water contacted with a halogen to increase the density to at least 9.0 lb/gal. (1.08 kg/L). Any suspended solids can be separated from the resulting halide brine.
  • Calcium bromide production in this test was a batch process, meaning that predetermined amounts of raw materials were added to the reactor in a stepwise fashion to produce a fixed amount of calcium bromide. When the reactions were complete, the product was removed from the reactor before adding the raw materials for the next batch.
  • the bromine scrubber system was checked to be running.
  • the damper valve to the reactor vent was opened to the scrubber system.
  • the hydrated lime controller was set for 9,310 lb (4,232 kg) hydrated lime addition.
  • the rotary valve speed control was set at 6 and the conveyer speed control at 6-7.
  • the bromine addition rate was adjusted to maintain batch color of light yellow with excess lime present. When the color went to red, the bromine pump was shut off and the lime charge was allowed to catch up to the bromine charge.
  • the reactor temperature was maintained at 185°F-210°F (85°C-100°C) by pumping the reactor contents through the heat exchanger.
  • 210°F 100.0°C
  • the bromine addition pump was shut off.
  • the bromine pump was turned back on when the temperature dropped below 195°F (90.6°C).
  • Hydrated lime was added to the reactor to bring the pH to 7.0-8.0 (10:1 dilution). About 20 min after adding lime, a sample was taken from the reactor to determine if the filtrate appeared clear white to slightly cloudy white and did not have an ammonia odor. Also, no yellow color was observed and the oxidation/reduction potential (ORP) was less than 200 mV. The final product was within its target pH and specific gravity range.
  • the heat exchanger was run until product temperature dropped to 150°F (65.6°C). If the product had required evaporation, the solution would have been pumped to the evaporator tank without further cooling.
  • the heat exchanger system was turned off, first shutting the raw product flow from tank to the heat exchanger by closing the valve next to reactor.
  • the coolant flow to the heat exchangers was turned off by turning pump off when the coolant glycol reached ambient temperature. Then the cooling fans were turned off.
  • the target density for filtered and cooled sample from the reactor was obtained.

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  • Inorganic Chemistry (AREA)
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Claims (29)

  1. Procédé de production d'une solution saline d'halogénure, comprenant :
    (a) l'addition d'un alcalin à un fluide aqueux ayant une densité supérieure à 8,30 livres/gallon (0,994 kg/litre) ;
    (b) l'addition d'un agent réducteur ; et
    (c) la mise en contact du fluide résultant de l'étape (b) avec l'halogène pour former une solution saline d'halogénure ;
    dans lequel la réaction est réalisée dans un réacteur conventionnel.
  2. Procédé de production d'une solution saline d'halogénure selon la revendication 1, dans lequel l'étape (a) et l'étape (b) de la revendication 1 consistent en une étape comprenant :
    (a) l'addition d'un alcalin et d'un agent réducteur à un fluide aqueux ayant une densité supérieure à 8,30 livres/gallon (0,994 kg/litre) ; et
    l'étape (c) consiste en :
    (c) la mise en contact du fluide résultant de l'étape (a) avec un halogène pour former une solution saline d'halogénure.
  3. Procédé de production d'une solution saline d'halogénure selon la revendication 1, dans lequel l'étape (a) et l'étape (c) consistent en l'étape de :
    (a) addition de chaux à un fluide aqueux ayant une densité supérieure à 8,30 livres/gallon (0,994 kg/litre) ;
    (c) mise en contact du fluide résultant de l'étape (b) avec un halogène pour augmenter la densité jusqu'à au moins 8,5 livres/gallon (1,02 kg/litre) ;
    et le procédé comprend en plus l'étape de :
    (d) séparation de toute matière solide suspendue par rapport aux fluides.
  4. Procédé selon l'une quelconque des revendications précédentes, dans lequel le fluide aqueux comprend de l'eau.
  5. Procédé selon la revendication 4, dans lequel l'eau est choisie parmi l'eau sensiblement pure, l'eau du robinet, l'eau de mer, l'eau des cours d'eau, l'eau de cuve, l'eau stagnante, les eaux usées, l'eau saumâtre, ou des combinaisons de celles-ci.
  6. Procédé selon la revendication 4, dans lequel l'eau est une eau claire.
  7. Procédé selon la revendication 1 ou 2, dans lequel l'alcalin est choisi parmi les hydroxydes de métaux alcalins, les oxydes de métaux alcalino-terreux, les hydroxydes de métaux alcalino-terreux, les oxydes métalliques de base, les hydroxydes métalliques de base et des combinaisons de ceux-ci.
  8. Procédé selon la revendication 7, dans lequel la source métallique des oxydes métalliques de base et hydroxydes métalliques de base est choisie parmi le fer, le zinc, le cuivre, le nickel, le cadmium, le cobalt, l'aluminium; le manganèse, le chrome et des combinaisons de ceux-ci.
  9. Procédé selon la revendication 7, dans lequel la source métallique des oxydes de métaux alcalino-terreux et des hydroxydes de métaux alcalino-terreux est choisie parmi le calcium, le magnésium, le strontium et des combinaisons de ceux-ci.
  10. Procédé selon l'une quelconque des revendications précédentes, dans lequel l'agent réducteur est l'ammoniac.
  11. Procédé selon l'une quelconque des revendications 1 à 9, dans lequel l'agent réducteur est l'acétaldéhyde.
  12. Procédé selon l'une quelconque des revendications 1 à 9, dans lequel l'agent réducteur est l'acide acétique.
  13. Procédé selon l'une quelconque des revendications précédentes, dans lequel l'halogène est choisi parmi le chlore, le brome ou l'iode.
  14. Procédé selon l'une quelconque des revendications précédentes, comprenant en outre l'étape de séparation des matières solides suspendues par rapport au fluide de départ.
  15. Procédé selon l'une quelconque des revendications précédentes, comprenant en outre l'étape de séparation des matières solides suspendues par rapport au fluide résultant.
  16. Procédé selon l'une quelconque des revendications précédentes, dans lequel la séparation des matières solides suspendues par rapport au fluide est réalisée dans un filtre par gravité.
  17. Procédé selon l'une quelconque des revendications précédentes, dans lequel la séparation des matières solides suspendues par rapport au fluide est réalisée dans un bassin de clarification.
  18. Procédé selon l'une quelconque des revendications précédentes, dans lequel la séparation des matières solides suspendues par rapport au fluide est réalisée dans une centrifugeuse.
  19. Procédé selon l'une quelconque des revendications précédentes, dans lequel la séparation des matières solides suspendues par rapport au fluide est réalisée dans un filtre sous vide.
  20. Procédé selon l'une quelconque des revendications précédentes, dans lequel la séparation des matières solides suspendues par rapport au fluide est réalisée dans un filtre sous pression.
  21. Procédé de production d'une solution saline d'halogénure selon la revendication 1, dans lequel l'étape (a) consiste en l'addition d'un alcalin à un fluide aqueux et l'étape (c) consiste en la mise en contact du fluide résultant de l'étape (b) avec du brome pour augmenter la densité jusqu'à au moins 8,5 livres/gallon (1,02 kg/litre) pour produire une solution saline de bromure.
  22. Procédé de production d'une solution saline d'halogénure selon la revendication 2, dans lequel l'étape (b) de la revendication 2 consiste en la mise en contact du fluide résultant de l'étape (a) avec du chlore pour augmenter la densité jusqu'à au moins 8,5 livres/gallon (1,02 kg/litre) pour produire une solution saline de chlorure.
  23. Procédé selon la revendication 22, dans lequel le fluide aqueux est l'eau et l'eau est choisie parmi l'eau sensiblement pure, l'eau du robinet, l'eau de mer, l'eau des cours d'eau, l'eau de cuve, l'eau stagnante, les eaux usées, l'eau saumâtre, ou des combinaisons de celles-ci.
  24. Procédé de production d'une solution saline d'halogénure selon la revendication 1, dans lequel l'étape (a) consiste en l'addition d'un alcalin à l'eau de mer et l'étape (c) consiste en la mise en contact du fluide résultant de l'étape (b) avec un halogène pour augmenter la densité jusqu'à au moins 9,0 livres/gallon (1,08 kg/litre) et, à l'étape (d), toute matière solide suspendue est séparée du fluide résultant de l'étape (c).
  25. Procédé de production d'une solution saline d'halogénure haute densité selon la revendication 3, dans lequel l'étape (b) et l'étape (c) consistent en :
    (b) l'addition d'ammoniac comme agent réducteur ; et
    (c) la mise en contact du fluide résultant de l'étape (b) avec du brome pour augmenter la densité jusqu'à au moins 10,0 livres/gallon (1,20 kg/litre) pour produire une solution saline de bromure, et à l'étape (d), les matières solides suspendues sont séparées du fluide résultant de l'étape (c).
  26. Procédé de production d'une solution saline d'halogénure selon la revendication 1, dans lequel l'étape (a) consiste en l'addition d'un alcalin à l'eau de mer et, à l'étape (b), l'ammoniac est ajoutée comme agent réducteur et l'halogène, à l'étape (c), est choisi parmi le chlore, le brome ou l'iode pour augmenter la densité jusqu'à au moins 9,0 livres/gallon (1,08 kg/litre) et, à l'étape (d), toute matière solide suspendue est séparée du fluide résultant de l'étape (c).
  27. Procédé de production d'une solution saline d'halogénure selon la revendication 1, dans lequel l'étape (a) consiste en l'addition d'un alcalin à l'eau de mer et, à l'étape (c), la densité est augmentée jusqu'à au moins 10,0 livres/gallon (1,20 kg/litre) et, à l'étape (d), toute matière solide suspendue est séparée du fluide résultant de l'étape (c).
  28. Procédé selon l'une quelconque des revendications précédentes, dans lequel la température est maintenue par recyclage du fluide à travers un échangeur de chaleur.
  29. Procédé de production d'une solution saline d'halogénure selon la revendication 1, dans lequel l'alcalin ajouté à l'étape (a) est choisi parmi les hydroxydes de métaux alcalins, les oxydes de métaux alcalino-terreux, les hydroxydes de métaux alcalino-terreux, les oxydes métalliques de base, les hydroxydes métalliques de base, et une combinaison de ceux-ci ; et à l'étape (b), l'agent réducteur est ajouté tout en maintenant la température à 68°F (20°C) ou au-dessus, et l'agent réducteur est choisi dans un groupe constitué de l'ammoniac, l'acétaldéhyde, l'acide acétique, et des combinaisons de ceux-ci ; et à l'étape (c), le densité est augmentée jusqu'à au moins 8,5 livres/gallon (1,02 kg/litre).
EP03716990A 2002-04-10 2003-04-04 Procede de production d'une saumure d'halogenure Expired - Lifetime EP1492728B1 (fr)

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US37129302P 2002-04-10 2002-04-10
US371293P 2002-04-10
PCT/US2003/010424 WO2003086972A1 (fr) 2002-04-10 2003-04-04 Procede de production d'une saumure d'halogenure

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US (1) US7087209B2 (fr)
EP (1) EP1492728B1 (fr)
IL (1) IL164333A0 (fr)
NO (1) NO20044708L (fr)
WO (1) WO2003086972A1 (fr)

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IL141661A (en) * 2001-02-26 2006-12-10 Bromine Compounds Ltd Process and facility for the production of bromine calcium by liquid-liquid extraction
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IL164333A0 (en) 2005-12-18
US7087209B2 (en) 2006-08-08
US20030198589A1 (en) 2003-10-23
WO2003086972A1 (fr) 2003-10-23
EP1492728A1 (fr) 2005-01-05
NO20044708L (no) 2004-10-29

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